Amino phosphine

ABSTRACT

A new P—N—P ligand in which each phosphorus atom is bonded to two ortho-fluorine substituted phenyl groups is useful in ethylene oligomerizations. In combination with i) a source of chromium and ii) an activator such as methalumoxane; the ligand of this invention may be used to prepare an oligomer product that contains a mixture of hexenes and octenes. The hexenes and octenes produced with this ligand contain very low levels of internal olefins when produced under preferred reaction conditions.

FIELD OF THE INVENTION

This invention provides a new P—N—P ligand. The ligand is useful inethylene oligomerization reactions.

BACKGROUND OF THE INVENTION

Alpha olefins are commercially produced by the oligomerization ofethylene in the presence of a simple alkyl aluminum catalyst (in the socalled “chain growth” process) or alternatively, in the presence of anorganometallic nickel catalyst (in the so called Shell Higher Olefins,or “SHOP” process). Both of these processes typically produce a crudeoligomer product having a broad distribution of alpha olefins with aneven number of carbon atoms (i.e. butene-1, hexene-1, octene-1 etc.).The various alpha olefins in the crude oligomer product are thentypically separated in a series of distillation columns. Butene-1 isgenerally the least valuable of these olefins as it is also produced inlarge quantities as a by-product in various cracking and refiningprocesses. Hexene-1 and octene-1 often command comparatively high pricesbecause these olefins are in high demand as comonomers for linear lowdensity polyethylene (LLDPE).

Technology for the selective trimerization of ethylene to hexene-1 hasbeen recently put into commercial use in response to the demand forhexene-1. The patent literature discloses catalysts which comprise achromium source and a pyrrolide ligand as being useful for thisprocess—see, for example, U.S. Pat. No. 5,198,563 (Reagen et al.,assigned to Phillips Petroleum).

Another family of highly active trimerization catalysts is disclosed byWass et al. in WO 02/04119 (now U.S. Pat. Nos. 7,143,633 and 6,800,702).The catalysts disclosed by Wass et al. are formed from a chromium sourceand a chelating diphosphine ligand and are described in further detailby Carter et al. (Chem. Comm. 2002, p 858-9). As described in the Chem.Comm. paper, these catalysts preferably comprise a diphosphine ligand inwhich both phosphine atoms are bonded to two phenyl groups that are eachsubstituted with an ortho-methoxy group. Hexene-1 is produced with highactivity and high selectivity by these catalysts.

Similar diphosphine/tetraphenyl ligands are disclosed by Blann et al. inWO04/056478 and WO 04/056479 (now US 2006/0229480 and US 2006/0173226).However, in comparison to the ligands of Wass et al., thedisphosphine/tetraphenyl ligands disclosed by Blann et al. generally donot contain polar substituents in ortho positions. The “tetraphenyl”diphosphine ligands claimed in the '480 application must not have orthosubstituents (of any kind) on all four of the phenyl groups and the“tetraphenyl” diphosphine ligands claimed in '226 are characterized byhaving a polar substituent in a meta or para position. Both of theseapproaches are shown to reduce the amount of hexenes produced andincrease the amount of octene (in comparison to the ligands of Wass etal.). However, the hexene fraction generally contains a large portion ofinternal hexenes, which is undesirable. Thus, chromium based catalystswhich contain the ligands of Wass et al. typically produce more octene(which may be advantageous if demand for octene is high) but theseligands have the disadvantage of producing a hexene stream which iscontaminated with a comparatively large amount of internal olefins.

Internal olefins are undesirable contaminants in linear low densitypolyethylene (LLDPE) production facilities because the internal olefinsare not readily incorporated into LLDPE with most transition metalcatalysts. Thus, it is preferable to remove/separate internal olefinsfrom alpha olefins if the alpha olefin is to be used in an LLDPEprocess. As will be appreciated by those skilled in the art, it iscomparatively difficult to separate hexene-1 from internal hexenes bydistillation due to the close boiling points of these hexene resins.

Accordingly, a process which selectively produces a mixture of hexene-1and octene-1 with very low levels of internal olefins represents adesirable addition to the art.

SUMMARY OF THE INVENTION

In one embodiment, the present invention provides a new molecule definedby the formula:

wherein R is isopropyl.

The molecule is particularly suitable for use as a ligand in a processto oligomerize ethylene. Potential alternative uses include ligands forhydrogenation and/or hydroformylation reactions.

Attempts to produce the new molecule by conventional condensationreactions (i.e., using a precursor amine and a precursor diphosphinechloride) were unsuccessful. Accordingly, another embodiment of thisinvention provides a new synthetic route to this molecule. A preferredsynthesis uses a molecule defined by the formula (ortho —F—C₆H₄)₂PXwherein X is chlorine and bromine and is described in more detail in theExamples.

Another embodiment of this invention provides a process to oligomerizeethylene. A process for the selective oligomerization of ethylene to amixture comprising hexene-1 and octene-1, said process comprisingcontacting ethylene under oligomerization reaction conditions with acatalyst system to produce an oligomerization product comprisinghexene-1 and octene-1, said catalyst system comprising:

-   -   i) a source of chromium;    -   ii) a ligand defined by the formula

-   -   wherein each of X₁ to X₄ is independently selected from the        group consisting of F, Br, or Cl; and each of R; ort¹ to ort⁴        and R₁ to R₁₂ is independently selected from the group        consisting of H and “non-interfering substituents” (i.e.        substituents that do not interfere with the oligomerization        reaction); and    -   iii) an activator.

In general, the ligand used in the oligomerization process of thisinvention has four ortho halide substituents—more specifically, each ofthe four phenyl groups has an ortho halide substituent. In the mostgeneral sense, each of ort¹ to ort⁴, X₁ to X₄ and R₁ to R₁₂ are hydrogenor “non-interfering substituents” (wherein the term simply means thatthe substituents do not interfere with the oligomerization process).

The oligomerization process of this invention may be conducted underconventional oligomerization conditions. One important advantage of thepresent invention is that the product olefins can comprise a desirablemixture of hexene and octene (in particular, greater than 80 weight % ofthe ethylene that is converted to a liquid product during the processcan be hexenes and octenes) with very low levels of internal olefins(preferably less than 15 weight % of the mixed hexene and octene streamis internal olefins) when the process is conducted under preferredtemperature and pressure conditions.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Part A Catalyst System

The catalyst system used in the process of the present invention mustcontain three essential components, namely:

-   -   (i) a source of chromium:    -   (ii) amino diphosphine ligand; and    -   (iii) an activator.

Preferred forms of each of these components are discussed below.

Chromium Source (“Component (i)”)

Any source of chromium which allows the oligomerization process of thepresent invention to proceed may be used. Preferred chromium sourcesinclude chromium trichloride; chromium (III) 2-ethylhexanoate; chromium(III) acetylacetonate and chromium carboxyl complexes such as chromiumhexacarboxyl.

Ligand Used in the Oligomerization Process (“Component (ii)”)

In general, the ligand used in the oligomerization process of thisinvention is defined by the formula:

wherein each of X₁ to X₄ is independently selected from the groupconsisting of F, Br, or Cl; and each of R; ort¹ to ort⁴ and R₁ to R₁₂ isindependently selected from the group consisting of H and“non-interfering substituents” (i.e. substituents that do not interferewith the oligomerization reaction).

Each of X₁ to X₄ is preferably fluorine.

R is preferably a hydrocarbyl group having from 1 to 30 carbon atoms.The hydrocarbyl groups may contain heteroatom substituents (having aheteroatom selected from O, N, P and S). Simple alkyl groups having from1 to 12 carbon atoms are preferred. Isopropyl is particularly preferred.

Each of ort¹ to ort⁴ is preferably selected from the group consisting ofH, Br, Cl, F and small alkyl groups (having from 1 to 3 carbon atoms). His most preferred.

Each of R₁ to R₁₂ is independently selected from the group consisting ofH, hydrocarbyl substituents which contain from 1 to 30 carbon atoms(which hydrocarbyl substituents may contain heteroatoms selected fromthe group consisting of O, N, P and S) and heteroatom substituents (i.e.substituents which are bonded to the phenyl ring via an O, N, P or Satom) which contain from 2 to 30 atoms. It is preferred that R₁ to R₁₂are not polar substituents. It is especially preferred that each of R₁to R₁₂ is selected from H and C₁ to C₆ alkyls or C₆ to C₁₂ aryls.

Activator (“Component (iii)”)

The activator (component (iii)) may be any compound that generates anactive catalyst for ethylene oligomerization with components (i) and(ii). Mixtures of activators may also be used. Suitable compoundsinclude organoaluminum compounds, organoboron compounds and inorganicacids and salts, such as tetrafluoroboric acid etherate, silvertetrafluoroborate, sodium hexafluoroantimonate and the like. Suitableorganoaluminium compounds include compounds of the formula AlR₃, whereeach R is independently C₁-C₁₂ alkyl, oxygen or halide, and compoundssuch as LiAlH₄ and the like. Examples include trimethylaluminium (TMA),triethylaluminium (TEA), tri-isobutylaluminium (TIBA),tri-n-octylaluminium, methylaluminium dichloride, ethylaluminiumdichloride, dimethylaluminium chloride, diethylaluminium chloride,ethylaluminiumsesquichloride, methylaluminiumsesquichloride, andalumoxanes. Alumoxanes are well known in the art as typically oligomericcompounds which can be prepared by the controlled addition of water toan alkylaluminium compound, for example trimethylaluminium. Suchcompounds can be linear, cyclic, cages or mixtures thereof. Commerciallyavailable alumoxanes are generally believed to be mixtures of linear andcyclic compounds. The cyclic alumoxanes can be represented by theformula [R⁶AlO]_(S) and the linear alumoxanes by the formulaR⁷(R⁸AlO)_(S) wherein s is a number from about 2 to 50, and wherein R⁶,R⁷, and R⁸ represent hydrocarbyl groups, preferably C₁ to C₆ alkylgroups, for example methyl, ethyl or butyl groups. Alkylalumoxanesespecially methylalumoxane (MAO) are preferred.

It will be recognized by those skilled in the art that commerciallyavailable alkylalumoxanes may contain a proportion of trialkylaluminium.For instance, commercial MAO usually contains approximately 10 wt %trimethylaluminium (TMA), and commercial “modified MAO” (or “MMAO”)contains both TMA and TIBA. Quantities of alkylalumoxane are generallyquoted herein on a molar basis of aluminium (and include such “free”trialkylaluminium).

Examples of suitable organoboron compounds are boroxines, NaBH₄,trimethylboron, triethylboron,dimethylphenylammoniumtetra(phenyl)borate, trityltetra(phenyl)borate,triphenylboron, dimethylphenylammonium tetra(pentafluorophenyl)borate,sodium tetrakis[(bis-3,5-trifluoromethyl)phenyl]borate,trityltetra(pentafluorophenyl)borate and tris(pentafluorophenyl) boron.

Activator compound (iii) may also be or contain a compound that acts asa reducing or oxidizing agent, such as sodium or zinc metal and thelike, or oxygen and the like.

In the preparation of the catalyst systems used in the presentinvention, the quantity of activating compound to be employed is easilydetermined by simple testing, for example, by the preparation of smalltest samples which can be used to oligimerize small quantities ofethylene and thus to determine the activity of the produced catalyst. Itis generally found that the quantity employed is sufficient to provide0.5 to 1000 moles of aluminium (or boron) per mole of chromium. MAO isthe presently preferred activator. Molar Al/Cr ratios of from 1/1 to500/1 are preferred.

Part B Process Conditions

The chromium (component (i)) and ligand (component (ii)) may be presentin any molar ratio which produces oligomer, preferably between 100:1 and1:100, and most preferably from 10:1 to 1:10, particularly 3:1 to 1:3.Generally the amounts of (i) and (ii) are approximately equal, i.e. aratio of between 1.5:1 and 1:1.5.

Components (i)-(iii) of the catalyst system utilized in the presentinvention may be added together simultaneously or sequentially, in anyorder, and in the presence or absence of ethylene in any suitablesolvent, so as to give an active catalyst. For example, components (i),(ii) and (iii) and ethylene may be contacted together simultaneously, orcomponents (i), (ii) and (iii) may be added together simultaneously orsequentially in any order and then contacted with ethylene, orcomponents (i) and (ii) may be added together to form an isolablemetal-ligand complex and then added to component (iii) and contactedwith ethylene, or components (i), (ii) and (iii) may be added togetherto form an isolable metal-ligand complex and then contacted withethylene. Suitable solvents for contacting the components of thecatalyst or catalyst system include, but are not limited to, hydrocarbonsolvents such as heptane, toluene, 1-hexene and the like, and polarsolvents such as diethyl ether, tetrahydrofuran, acetonitrile,dichloromethane, chloroform, chlorobenzene, methanol, acetone and thelike.

The catalyst components (i), (ii) and (iii) utilized in the presentinvention can be unsupported or supported on a support material, forexample, silica, alumina, MgCl₂ or zirconia, or on a polymer, forexample polyethylene, polypropylene, polystyrene, or poly(aminostyrene).If desired the catalysts can be formed in situ in the presence of thesupport material, or the support material can be pre-impregnated orpremixed, simultaneously or sequentially, with one or more of thecatalyst components. The quantity of support material employed can varywidely, for example from 100,000 to 1 grams per gram of metal present inthe transition metal compound. In some cases, the support may materialcan also act as or as a component of the activator compound (iii).Examples include supports containing alumoxane moieties.

The oligomerization can be, conducted under solution phase, slurryphase, gas phase or bulk phase conditions. Suitable temperatures rangefrom 10° C. to +300° C. preferably from 10° C. to 100° C., especiallyfrom 20 to 70° C. Suitable pressures are from atmospheric to 800atmospheres (gauge) preferably from 5 atmospheres to 100 atmospheres,especially from 10 to 50 atmospheres.

Irrespective of the process conditions employed, the oligomerization istypically carried out under conditions that substantially excludeoxygen, water, and other materials that act as catalyst poisons. Also,oligomerization can be carried out in the presence of additives tocontrol selectivity, enhance activity and reduce the amount of polymerformed in oligomerization processes. Potentially suitable additivesinclude, but are not limited to, hydrogen or a halide source.

There exist a number of options for the oligomerization reactorincluding batch, semi-batch, and continuous operation. The reactions ofthe present invention can be performed under a range of processconditions that are readily apparent to those skilled in the art: as ahomogeneous liquid phase reaction in the presence or absence of an inerthydrocarbon diluent such as toluene or heptanes; as a two-phaseliquid/liquid reaction; as a slurry process where the catalyst is in aform that displays little or no solubility; as a bulk process in whichessentially neat reactant and/or product olefins serve as the dominantmedium; as a gas-phase process in which at least a portion of thereactant or product olefin(s) are transported to or from a supportedform of the catalyst via the gaseous state. Evaporative cooling from oneor more monomers or inert volatile liquids is but one method that can beemployed to effect the removal of heat from the reaction. The reactionsmay be performed in the known types of gas-phase reactors, such ascirculating bed, vertically or horizontally stirred-bed, fixed-bed, orfluidized-bed reactors, liquid-phase reactors, such as plug-flow,continuously stirred tank, or loop reactors, or combinations thereof. Awide range of methods for effecting product, reactant, and catalystseparation and/or purification are known to those skilled in the art andmay be employed: distillation, filtration, liquid-liquid separation,slurry settling, extraction, etc. One or more of these methods may beperformed separately from the oligomerization reaction or it may beadvantageous to integrate at least some with the reaction; anon-limiting example of this would be a process employing catalytic (orreactive) distillation. Also advantageous may be a process whichincludes more than one reactor, a catalyst kill system between reactorsor after the final reactor, or an integrated reactor/separator/purifier.While all catalyst components, reactants, inerts, and products could beemployed in the present invention on a once-through basis, it is ofteneconomically advantageous to recycle one or more of these materials; inthe case of the catalyst system, this might require reconstituting oneor more of the catalysts components to achieve the active catalystsystem. It is within the scope of this invention that an oligomerizationproduct might also serve as a solvent or diluent. Mixtures of inertdiluents or solvents also could be employed. The preferred diluents orsolvents are aliphatic and aromatic hydrocarbons and halogenatedhydrocarbons such as, for example, isobutane, pentane, toluene, xylene,ethylbenzene, cumene, mesitylene, heptane, cyclohexane,methylcyclohexane, 1-hexene, 1-octene, chlorobenzene, dichlorobenzene,and the like, and mixtures such as Isopar™.

Techniques for varying the distribution of products from theoligomerization reactions include controlling process conditions (e.g.concentration of components (i)-(iii), reaction temperature, pressure,residence time) and properly selecting the design of the process and arewell known to those skilled in the art.

The ethylene feedstock for the oligomerization may be substantially pureor may contain other olefinic impurities and/or ethane. One embodimentof the process of the invention comprises the oligomerization ofethylene-containing waste streams from other chemical processes or acrude ethylene/ethane mixture from a cracker.

In a highly preferred embodiment of the present invention, theoligomerization product produced from this invention is added to aproduct stream from another alpha olefins manufacturing process forseparation into different alpha olefins. As previously discussed,“conventional alpha olefin plants” (wherein the term includes i) thoseprocesses which produce alpha olefins by a chain growth process using analuminum alkyl catalyst, ii) the aforementioned “SHOP” process and iii)the production of olefins from synthesis gas using the so called Lurgiprocess) have a series of distillation columns to separate the “crudealpha product” (i.e. a mixture of alpha olefins) into alpha olefins(such as butene-1, hexene-1 and octene-1). The mixed hexene-octeneproduct which is produced in accordance with the present invention ishighly suitable for addition/mixing with a crude alpha olefin productfrom an existing alpha olefin plant (or a “cut” or fraction of theproduct from such a plant) because the mixed hexene-octene productproduced in accordance with the present invention can have very lowlevels of internal olefins. Thus, the hexene-octene product of thepresent invention can be readily separated in the existing distillationcolumns of alpha olefin plants (without causing the large burden on theoperation of these distillation columns which would otherwise exist ifthe present hexene-octene product stream contained large quantities ofinternal olefins). As used herein, the term “liquid product” is meant torefer to the oligomers produced by the process of the present inventionwhich have from 4 to (about) 20 carbon atoms.

The liquid product from the oligomerization process of the presentinvention preferably consists of from 20 to 80 weight % octenes(especially from 35 to 75 weight %) octenes and from 15 to 50 weight %(especially from 20 to 40 weight %) hexenes (where all of the weight %are calculated on the basis of the liquid product by 100%.

The preferred oligomerization process of this invention is alsocharacterized by producing very low levels of internal olefins (i.e. lowlevels of hexene-2, hexene-3, octene-2, octene-3 etc.), with preferredlevels of less than 10 weight % (especially less than 5 weight %) of thehexenes and octenes being internal olefins.

One embodiment of the present invention encompasses the use ofcomponents (i) (ii) and (iii) in conjunction with one or more types ofolefin polymerization catalyst system (iv) to trimerise ethylene andsubsequently incorporate a portion of the trimerisation product(s) intoa higher polymer.

Component (iv) may be one or more suitable polymerization catalystsystem(s), examples of which include, but are not limited to,conventional Ziegler-Natta catalysts, metallocene catalysts,monocyclopentadienyl or “constrained geometry” catalysts, phosphiniminecatalysts, heat activated supported chromium oxide catalysts (e.g.“Phillips”-type catalysts), late transition metal polymerizationcatalysts (eg. diimine, diphosphine and salicylaldimine nickel/palladiumcatalysts, iron and cobalt pyridyldiimine catalysts and the like) andother so-called “single site catalysts” (SSC's).

Ziegler-Natta catalysts, in general, consist of two main components. Onecomponent is an alkyl or hydride of a Group I to III metal, mostcommonly Al(Et)₃ or Al(iBu)₃ or Al(Et)₂Cl but also encompassing Grignardreagents, n-butyllithium, or dialkylzinc compounds. The second componentis a salt of a Group IV to VIII transition metal, most commonly halidesof titanium or vanadium such as TiCl₄, TiCl₃, VCl₄, or VOCl₃. Thecatalyst components when mixed, usually in a hydrocarbon solvent, mayform a homogeneous or heterogeneous product. Such catalysts may beimpregnated on a support, if desired, by means known to those skilled inthe art and so used in any of the major processes known forco-ordination catalysis of polyolefins such as solution, slurry, andgas-phase. In addition to the two major components described above,amounts of other compounds (typically electron donors) maybe added tofurther modify the polymerization behaviour or activity of the catalyst.

Metallocene catalysts, in general, consist of transition metalcomplexes, most commonly based on Group IV metals, ligated withcyclopentadienyl(Cp)-type groups. A wide range of structures of thistype of catalysts is known, including those with substituted, linkedand/or heteroatom-containing Cp groups, Cp groups fused to other ringsystems and the like. Additional activators, such as boranes oralumoxane, are often used and the catalysts may be supported, ifdesired.

Monocyclopentadienyl or “constrained geometry” catalysts, in general,consist of a transition metal complexes, most commonly based on Group IVmetals, ligated with one cyclopentadienyl(Cp)-type group, often linkedto additional donor group. A wide range of structures of this type ofcatalyst is known, including those with substituted, linked and/orheteroatom-containing Cp groups, Cp groups fused to other ring systemsand a range of linked and non-linked additional donor groups such asamides, amines and alkoxides. Additional activators, such as boranes oralumoxane, are often used and the catalysts may be supported, ifdesired.

A typical heat activated chromium oxide (Phillips) type catalyst employsa combination of a support material to which has first been added achromium-containing material wherein at least part of the chromium is inthe hexavalent state by heating in the presence of molecular oxygen. Thesupport is generally composed of about 80 to 100 wt. % silica, theremainder, if any, being selected from the group consisting ofrefractory metal oxides, such as aluminium, boria, magnesia, thoria,zirconia, titania and mixtures of two or more of these refractory metaloxides. Supports can also comprise alumina, aluminium phosphate, boronphosphate and mixtures thereof with each other or with silica. Thechromium compound is typically added to the support as a chromium (III)compound such as the acetate or acetylacetonate in order to avoid thetoxicity of chromium (VI). The raw catalyst is then calcined in air at atemperature between 250 and 1000° C. for a period of from a few secondsto several hours. This converts at least part of the chromium to thehexavalent state. Reduction of the Cr (VI) to its active form normallyoccurs in the polymerization reaction, but can be done at the end of thecalcination cycle with CO at about 350° C. Additional compounds, such asfluorine, aluminium and/or titanium may be added to the raw Phillipscatalyst to modify it.

Late transition metal and single site catalysts cover a wide range ofcatalyst structures based on metals across the transition series.

Component (iv) may also comprise one or more polymerization catalysts orcatalyst systems together with one or more additional oligomerizationcatalysts or catalyst systems. Suitable oligomerization catalystsinclude, but are not limited to, those that dimerise (for example,nickel phosphine dimerisation catalysts) or trimerise olefins orotherwise oligomerize olefins to, for example, a broader distribution of1-olefins (for example, iron and cobalt pyridyldiimine oligomerizationcatalysts).

Component (iv) may independently be supported or unsupported. Wherecomponents (i) and (ii) and optionally (iii) are supported, (iv) may beco-supported sequentially in any order or simultaneously on the samesupport or may be on a separate support. For some combinations, thecomponents (i) (iii) may be part or all of component (iv). For example,if component (iv) is a heat activated chromium oxide catalyst then thismay be (i), a chromium source and if component (iv) contains analumoxane activator then this may also be the optional activator (iii).

The components (i), (ii), (iii) and (iv) may be in essentially any molarratio that produces a polymer product. The precise ratio requireddepends on the relative reactivity of the components and also on thedesired properties of the product or catalyst systems.

An “in series” process could be conducted by first conducting theoligomerization reaction, then passing the oligomerization product to apolymerization reaction. In the case of an “in series” process variouspurification, analysis and control steps for the oligomeric productcould potentially be incorporated between the trimerization andsubsequent reaction stages. Recycling between reactors configured inseries is also possible. An example of such a process would be theoligomerization of ethylene in a single reactor with a catalystcomprising components (i)-(iii) followed by co-polymerization of theoligomerization product with ethylene in a separate, linked reactor togive branched polyethylene. Another example would be the oligomerizationof an ethylene-containing waste stream from a polyethylene process,followed by introduction of the oligomerization product back into thepolyethylene process as a co-monomer for the production of branchedpolyethylene.

An example of an “in situ” process is the production of branchedpolyethylene catalyzed by components (i)-(iv), added in any order suchthat the active catalytic species derived from components (i)-(iii) areat some point present in a reactor with component (iv).

Both the “in series and “in situ” approaches can be adaptions of currentpolymerization technology for the process stages including component(iv). All major olefin existing polymerization processes, includingmultiple reactor processes, are considered adaptable to this approach.One adaption is the incorporation of an oligomerization catalyst bedinto a recycle loop of a gas phase polymerization process, this could beas a side or recycle stream within the main fluidization recycle loopand or within the degassing recovery and recycle system.

Polymerization conditions when component (iv) is present can be, forexample, solution phase, slurry phase, gas phase or bulk phase, withtemperatures ranging from −100° C. to +300° C., and at pressures ofatmospheric and above, particularly from 1.5 to 50 atmospheres. Reactionconditions, will typically have a significant impact upon the properties(e.g. density, melt index, yield) of the polymer being made and it islikely that the polymer requirements will dictate many of the reactionvariables. Reaction temperature, particularly in processes where it isimportant to operate below the sintering temperature of the polymer,will typically, and preferably, be primarily selected to optimize thepolymerization reaction conditions. Also, polymerization orcopolymerization can be carried out in the presence of additives tocontrol polymer or copolymer molecular weights. The use of hydrogen gasas a means of controlling the average molecular weight of the polymer orcopolymer applies generally to the polymerization process of the presentinvention.

Slurry phase polymerization conditions or gas phase polymerizationconditions are particularly useful for the production of high or lowdensity grades of polyethylene, and polypropylene. In these processesthe polymerization conditions can be batch, continuous orsemi-continuous. Furthermore, one or more reactors may be used, e.g.from two to five reactors in series. Different reaction conditions, suchas different temperatures or hydrogen concentrations may be employed inthe different reactors.

Once the polymer product is discharged from the reactor, any associatedand absorbed hydrocarbons are substantially removed, or degassed, fromthe polymer by, for example, pressure let-down or gas purging usingfresh or recycled steam, nitrogen or light hydrocarbons (such asethylene). Recovered gaseous or liquid hydrocarbons may be recycled to apurification system or the polymerization zone.

In the slurry phase polymerization process the polymerization diluent iscompatible with the polymer(s) and catalysts, and may be an alkane suchas hexane, heptane, isobutane, or a mixture of hydrocarbons orparaffins. The polymerization zone can be, for example, an autoclave orsimilar reaction vessel, or a continuous liquid full loop reactor, e.g.of the type well-known in the manufacture of polyethylene by thePhillips Process. When the polymerization process of the presentinvention is carried out under slurry conditions the polymerization ispreferably carried out at a temperature above 0° C., most preferablyabove 15° C. Under slurry conditions the polymerization temperature ispreferably maintained below the temperature at which the polymercommences to soften or sinter in the presence of the polymerizationdiluent. If the temperature is allowed to go above the lattertemperature, fouling of the reactor can occur. Adjustment of thepolymerization within these defined temperature ranges can provide auseful means of controlling the average molecular weight of the producedpolymer. A further useful means of controlling the molecular weight isto conduct the polymerization in the presence of hydrogen gas which actsas chain transfer agent. Generally, the higher the concentration ofhydrogen employed, the lower the average molecular weight of theproduced polymer.

In bulk polymerization processes, liquid monomer such as propylene isused as the polymerization medium.

Methods for operating gas phase polymerization processes are well knownin the art. Such methods generally involve agitating (e.g. by stirring,vibrating or fluidizing) a bed of catalyst, or a bed of the targetpolymer (i.e. polymer having the same or similar physical properties tothat which it is desired to make in the polymerization process)containing a catalyst, and feeding thereto a stream of monomer (underconditions such that at least part of the monomer polymerizes in contactwith the catalyst in the bed. The bed is generally cooled by theaddition of cool gas (e.g. recycled gaseous monomer) and/or volatileliquid (e.g. a volatile inert hydrocarbon, or gaseous monomer which hasbeen condensed to form a liquid). The polymer produced in, and isolatedfrom, gas phase processes forms directly a solid in the polymerizationzone and is free from, or substantially free from liquid. As is wellknown to those skilled in the art, if any liquid is allowed to enter thepolymerization zone of a gas phase polymerization process the quantityof liquid in the polymerization zone is small in relation to thequantity of polymer present. This is in contrast to “solution phase”processes wherein the polymer is formed dissolved in a solvent, and“slurry phase” processes wherein the polymer forms as a suspension in aliquid diluent.

The gas phase process can be operated under batch, semi-batch, orso-called “continuous” conditions. It is preferred to operate underconditions such that monomer is continuously recycled to an agitatedpolymerization zone containing polymerization catalyst, make-up monomerbeing provided to replace polymerized monomer, and continuously orintermittently withdrawing produced polymer from the polymerization zoneat a rate comparable to the rate of formation of the polymer, freshcatalyst being added to the polymerization zone to replace the catalystwithdrawn from the polymerization zone with the produced polymer.

Methods for operating gas phase fluidized bed processes for makingpolyethylene, ethylene copolymers and polypropylene are well known inthe art. The process can be operated, for example, in a verticalcylindrical reactor equipped with a perforated distribution plate tosupport the bed and to distribute the incoming fluidizing gas streamthrough the bed. The fluidizing gas circulating through the bed servesto remove the heat of polymerization from the bed and to supply monomerfor polymerization in the bed. Thus the fluidizing gas generallycomprises the monomer(s) normally together with some inert gas (e.g.nitrogen or inert hydrocarbons such as methane, ethane, propane, butane,pentane or hexane) and optionally with hydrogen as molecular weightmodifier. The hot fluidizing gas emerging from the top of the bed is ledoptionally through a velocity reduction zone (this can be a cylindricalportion of the reactor having a wider diameter) and, if desired, acyclone and or filters to disentrain fine solid particles from the gasstream. The hot gas is then led to a heat exchanger to remove at leastpart of the heat of polymerization. Catalysts are preferably fedcontinuously or at regular internals to the bed. At start up of theprocess, the bed comprises fluidizable polymer which is preferablysimilar to the target polymer. Polymer is produced continuously withinthe bed by the polymerization of the monomer(s). Preferably means areprovided to discharge polymer from the bed continuously or at regularinternals to maintain the fluidized bed at the desired height. Theprocess is generally operated at relatively low pressure, for example,at 10 to 50 atmospheres, and at temperatures for example, between 50 and135° C. The temperature of the bed is maintained below the sinteringtemperature of the fluidized polymer to avoid problems of agglomeration.

In the gas phase fluidized bed process for polymerization of olefins theheat evolved by the exothermic polymerization reaction is normallyremoved from the polymerization zone (i.e. the fluidized bed) by meansof the fluidizing gas stream as described above. The hot reactor gasemerging from the top of the bed is led through one or more heatexchangers wherein the gas is cooled. The cooled reactor gas, togetherwith any make-up gas, is then recycled to the base of the bed. In thegas phase fluidized bed polymerization process of the present inventionit is desirable to provide additional cooling of the bed (and therebyimprove the space time yield of the process) by feeding a volatileliquid to the bed under conditions such that the liquid evaporates inthe bed thereby absorbing additional heat of polymerization from the bedby the “latent heat of evaporation” effect. When the hot recycle gasfrom the bed enters the beat exchanger, the volatile liquid can condenseout. In one embodiment of the present invention the volatile liquid isseparated from the recycle gas and reintroduced separately into the bed.Thus, for example, the volatile liquid can be separated and sprayed intothe bed. In another embodiment of the present invention the volatileliquid is recycled to the bed with the recycle gas. Thus the volatileliquid can be condensed from the fluidizing gas stream emerging from thereactor and can be recycled to the bed with recycle gas, or can beseparated from the recycle gas and then returned to the bed.

A number of process options can be envisaged when using the catalysts ofthe present invention in an integrated process to prepare higherpolymers i.e. when component (iv) is present. These options include “inseries” processes in which the oligomerization and subsequentpolymerization are carried in separate but linked reactors and “in situ”processes in which a both reaction steps are carried out in the samereactor.

In the case of a gas phase “in situ” polymerization process, component(iv) can, for example, be introduced into the polymerization reactionzone in liquid form, for example, as a solution in a substantially inertliquid diluent. Components (i)-(iv) may be independently added to anypart of the polymerization reactor simultaneously or sequentiallytogether or separately. Under these circumstances it is preferred theliquid containing the component(s) is sprayed as fine droplets into thepolymerization zone. The droplet diameter is preferably within the range1 to 1000 microns.

Although not usually required, upon completion of polymerization orcopolymerization, or when it is desired to terminate polymerization orcopolymerization or at least temporarily deactivate the catalyst orcatalyst component of this invention, the catalyst can be contacted withwater, alcohols, acetone, or other suitable catalyst deactivators amanner known to persons of skill in the art.

A range of polyethylene polymers are considered accessible includinghigh density polyethylene, medium density polyethylene, low densitypolyethylene, ultra low density polyethylene and elastomeric materials.Particularly important are the polymers having a density in the range of0.91 to 0.93, grams per cubic centimeter (g/cc) generally referred to inthe art as linear low density polyethylene. Such polymers and copolymersare used extensively in the manufacture of flexible blown or cast film.

Depending upon the use of the polymer product, minor amounts ofadditives are typically incorporated into the polymer formulation suchas acid scavengers, antioxidants, stabilizers, and the like. Generally,these additives are incorporated at levels of about 25 to 2000 parts permillion by weight (ppm), typically from about 50 to about 1000 ppm, andmore typically 400 to 1000 ppm, based on the polymer. In use, polymersor copolymers made according to the invention in the form of a powderare conventionally compounded into pellets. Examples of uses for polymercompositions made according to the invention include use to form fibres,extruded films, tapes, spunbonded webs, molded or thermoformed products,and the like. The polymers may be blown or cast into films, or may beused for making a variety of molded or extruded articles such as pipes,and containers such as bottles or drums. Specific additive packages foreach application may be selected as known in the art. Examples ofsupplemental additives include slip agents, anti-blocks, anti-stats,mould release agents, primary and secondary anti-oxidants, clarifiers,nucleants, uv stabilizers, and the like. Classes of additives are wellknown in the art and include phosphite antioxidants, hydroxylamine (suchas N,N-dialkyl hydroxylamine) and amine oxide (such as dialkyl methylamine oxide) antioxidants, hindered amine light (uv) stabilizers,phenolic stabilizers, benzofuranone stabilizers, and the like.

Fillers such as silica, glass fibers, talc, and the like, nucleatingagents, and colourants also may be added to the polymer compositions asknown by the art.

The present invention is illustrated in more detail by the followingnon-limiting examples.

EXAMPLES

The following abbreviations are used in the examples:

A=Angstrom unitsNMR=nuclear magnetic resonanceEt=ethylBu=butyliPr=isopropylc*=comparativerpm=revolutions per minuteGC=gas chromatographyR_(x)=reactionWt=weightC₄'s=butenesC₆'s=hexenesC₈'s=octenesPE=polyethylene

Ligand Synthesis General

All reactions involving air and or moisture sensitive compounds wereconducted under nitrogen using standard Schlenk or cannula techniques,or in a glovebox. Reaction solvents were purified prior to use (e.g. bydistillation) and stored over activated 4 Å sieves. Diethylamine,triethylamine and isopropylamine were purchased from Aldrich and driedover 4 Å molecular sieves prior to use. 1-Bromo-2-fluoro-benzene,phosphorus trichloride (PCl₃), hydrogen chloride gas and n-butyllithiumwere purchased from Aldrich and used as is. The methalumoxane (MAO), 10wt % Al in toluene, was purchased from Akzo and used as is. Deuteratedsolvents were purchased (toluene-d₈, THF-d₈) and were stored over 4 Åsieves. NMR spectra were recorded on a Bruker 300 MHz spectrometer(300.1 MHz for ¹H, 121.5 MHz for ³¹P, 282.4 for ¹⁹F).

Preparation of Et₂NPCl₂

Et₂NH (50.00 mmol, 5.17 mL) was added dropwise to a solution of PCl₃(25.00 mmol, 2.18 mL) in diethyl ether (will use “ether” from here) (200mL) at −78° C. After the addition, the cold bath was removed and theslurry was allowed to warm to room temperature over 2 hours. The slurrywas filtered and the filtrate was pumped to dryness. The residue wasdistilled (500 microns, 55° C.) to give the product in quantitativeyield.

¹H NMR (δ, toluene-d₈): 2.66 (doublet of a quartets, 4H, J_(PH)=13 Hz,J_(HH)=7 Hz), 0.75 (triplet, 6H, J=7 Hz).

Preparation of (ortho-F—C₆H₄)₂P-NEt₂

To solution of n-BuLi (17.00 mL of 1.6 M n-BuLi hexane solution, 27.18mmol) in ether (100 mL) maintained at −85° C., was added dropwise asolution of 1-bromo-2-fluorobenzene (4.76 g, 27.18 mmol) in ether (40mL) over 2 hours. After addition, the reaction flask was stirred for 1hour at −78° C., resulting in a white slurry. Et₂NPCl₂ (2.36 g, 13.58mmol) in ether (20 mL) was then added very slowly while the reactiontemperature was maintained at −85° C. The reaction was allowed to warmto −10° C. overnight. Toluene (10 mL) was then added to the reactionflask and the volatiles were removed in vacuo. The residue was extractedwith toluene and the solution was pumped to dryness. The crude productwas distilled (300 microns, 100° C.) yielding 3.78 g (95%) of product.¹H NMR (δ, THF-d₈): 7.40-7.01 (4 equal intense multiplets, 8H), 3.11(doublets of quartet, 4H, J_(PH)=13 Hz, J_(HH)=7 Hz), 0.97 (triplet, 6H,J=7 Hz). ¹⁹F NMR (δ, THF-d₈): −163.21 (doublet of multiplets, J=48 Hz).GC-MS. M⁺=293.

Preparation of (ortho-F—C₆H₄)₂PCl

Anhydrous HCl(g) was introduced to the head space of an etherealsolution (100 mL) of (ortho-F—C₆H₄)P-NEt₂ (3.73 g, 12.70 mmol) to apressure of 3 psi. A white precipitate formed immediately. The reactionwas stirred for an additional 0.5 hours at which point the slurry waspumped to dryness to remove volatiles. The residue was re-slurried inether (100 mL) and filtered. The filtrate was pumped to dryness yielding(ortho-F—C₆H₄)₂PCl as a colorless oil in quantitative yield. ¹H NMR (δ,THF-d₈): 7.60 (m, 4H), 7.20 (m, 2H), 7.08 (m, 2H). ¹⁹F NMR (δ, THF-d₈):−106.94 (doublet of multiplets, J=67 Hz).

Preparation of (ortho-F—C₆H₄)₂PNH(i-Pr)

To a solution of (ortho-F—C₆H₄)PCl (1.00 g, 3.90 mmol) in ether (50 mL)and NEt₃ (3 mL) was added an ethereal solution of i-PrNH₂ (0.42 mL, 4.90mmol) at −5° C. Immediate precipitate was observed. The slurry wasstirred for 3 hours and filtered. The filtrate was pumped to dryness togive a colorless oil of (ortho-F—C₆H₄)PNH(i-Pr) in quantitative yield.

¹H NMR (δ, THF-d₈): 7.42 (m, 2H), 7.30 (m, 2H), 7.11 (m, 2H), 6.96 (m,2H), 3.30 (septet, 1H, J=7 Hz), 2.86 (brs, 1H), 1.15 (d, 6H, J=7 Hz).¹⁹F NMR (δ, THF-d₈): −109.85 (doublet of multiplets, J=40 Hz). GC-MS,M⁺=279.

Preparation of (ortho-F—C₆H)₂PN (i-Pr)P(ortho-F—C₆H₄)₂

To a solution of (ortho-F—C₆H₄)₂PNH(i-Pr) (3.90 mmol) [made from i-PrNH₂and (ortho-F—C₆H₄)₂PCl (1.00 g, 3.90 mmol)] in ether (100 mL) maintainedat −70° C. was added dropwise a solution of n-BuLi (2.43 mL of 1.6 Mn-BuLi hexane solution, 3.90 mmol)). The mixture was stirred at −70° C.for 1 hour and allowed to warm to −10° C. in a cold bath (2 hours). Thesolution was re-cooled to −70° C. and (ortho-F—C₆H₄)₂PCl (1.00 g, 3.90mmol) was slowly added. The solution was stirred for 1 hour at −70° C.and allowed to slowly warm to room temperature forming a whiteprecipitate. The slurry was pumped to dryness and the residue wasextracted with toluene and filtered. The filtrate was pumped to drynessand recrystallized from heptane at −70° C. (2×) yielding 1.13 g (58%) ofproduct. At room temperature this material was an oil which containedboth the desired ligand (ortho-F—C₆H₄)₂PN(i-Pr)P(ortho-F—C₆H₄)₂ and itsisomer (ortho-F—C₆H₄)₂P[═N(i-Pr]P(ortho-F—C₆H₄)₂. A toluene solution ofthis mixture and 50 mg of (ortho-F—C₆H₄)₂PCl was heated at 65° C. forthree hours to convert the isomer to the desired ligand. ¹H NMR (THF-d8,δ): 7.35 (m, 8H), 7.10 (m, 4H), 6.96 (m, 4H), 3.94 (m, 1H), 1.24 (d, 6H,J=7 Hz). ¹⁹F NMR (THF-d₈, δ): −104.2 (br. s).

In a more preferred procedure the initial steps of the synthesis areconducted in pentane at −5° C. (instead of ether) with 10% more of the(ortho-F—C₆H₄)₂PCl (otherwise as described above). This preferredprocedure allows (ortho-F—C₆H₄)₂PN(i-Pr)P(ortho-F—C₆H₄)₂ to be formed inhigh (essentially quantitative) yield without the final step of heatingin toluene.

(ortho-F—C₆H₄)₂PN(i-Pr)P(ortho-F—C₆H₄)₂ is a novel molecule and isclaimed, per se, in claim 1.

Oligomerization Reactions Example 1

A 600-mL reactor fitted with a gas-entrained stirrer (1700 rpm) waspurged 3 times with argon while heated at 50° C. The reactor was thencooled to 30° C. and a solution of MAO (11.72 g, 10 wt % Al) in 57.31 gof toluene, followed by 86.7 g of toluene was transferred via astainless steel cannula to the reactor. The reactor was then pressurizedwith ethylene (15 atmospheres (gauge)) and the temperature adjusted to45° C. Bis(di-(ortho-fluorophenyl)phosphino)-1-propylamine (33.4 mg,0.067 mmol) in 8.69 g of toluene was added to chromium acetylacetonate(22.9 mg, 0.066 mmol) in 8.68 g of toluene in a hypovial. The mixturewas sonicated at ambient temperature for 1 minute and then transferredunder ethylene to the pressurized reactor. Immediately after, additionalethylene was added to increase the reactor pressure to 20 atmospheres(gauge). The reaction was terminated after 12 minutes by stopping theflow of ethylene to the reactor and cooling the contents to 30° C., atwhich point excess ethylene was slowly released from the reactor coolingthe contents to 0° C. The product mixture was transferred to apre-weighed flask containing 1 g of ethanol. A sample of the liquidproduct was analyzed by GC. The solid products were collected, weighedand dried at ambient temperature. The mass of the total product wasobtained by summing the weight of liquid and wet solid fractions (50.2g) (Example 1, Table 1).

Example 2

A 600 mL reactor fitted with a gas-entrained stirrer (1700 rpm) waspurged 3 times with argon while heated at 75° C. The reactor was thencooled to 30° C. and a solution of MAO (11.69 g, 10 wt % Al) in 57.41 gtoluene, followed by 86.62 g of toluene was transferred via a stainlesssteel cannula to the reactor. The reactor was then pressurized withethylene (15 atmospheres (gauge)) and the temperature adjusted to 70° C.Bis(di-(ortho-fluorophenyl)phosphino)-1-propylamine (33.5 mg, 0.067mmol) in 8.69 g of toluene was added to chromium acetylacetonate (22.8mg, 0.065 mmol) in 8.70 g of toluene in a hypovial. The mixture wassonicated at ambient temperature for 1 minute and then transferred underethylene to the pressurized reactor. Immediately after, additionalethylene was added to increase the reactor pressure to 20 atmospheres(gauge). The reaction was terminated after 21 minutes by stopping theflow of ethylene to the reactor and cooling the contents to 30° C., atwhich point excess ethylene was slowly released from the reactor coolingthe contents to 0° C. The product mixture was transferred to apre-weighed flask containing 1 g of ethanol. A sample of the liquidproduct was analyzed by GC. The solid products were collected, weighedand dried at ambient temperature. The mass of the total product wasobtained by summing the weight of liquid and wet solid fractions (28.0g) (Example 2, Table 1).

Example 3

A 600 mL reactor fitted with a gas-entrained stirrer (1700 rpm) waspurged 3 times with argon while heated at 50° C. The reactor was thencooled to 30° C. and a solution of MAO (11.70 g, 10 wt % Al) in 57.32 gtoluene, followed by 86.7 g of toluene was transferred via a stainlesssteel cannula to the reactor. The reactor was then pressurized withethylene (35 atmospheres (gauge)) and the temperature adjusted to 45° C.Bis(di-(ortho-fluorophenyl)phosphino)-1-propylamine (33.5 mg, 0.067mmol) in 8.70 g of toluene was added to chromium acetylacetonate (22.8mg, 0.065 mmol) in 8.68 g of toluene in a hypovial. The mixture wassonicated at ambient temperature for 1 minute and then transferred underethylene to the pressurized reactor. Immediately after, additionalethylene was added to increase the reactor pressure to 40 atmospheres(gauge). The reaction was terminated after 5 minutes by stopping theflow of ethylene to the reactor and cooling the contents to 30° C., atwhich point excess ethylene was slowly released from the reactor coolingthe contents to 0° C. The product mixture was transferred to apre-weighed flask containing 1 g of ethanol. A sample of the liquidproduct was analyzed by GC. The solid products were collected, weighedand dried at ambient temperature. The mass of the total product wasobtained by summing the weight of liquid and wet solid fractions (47.2g) (Example 3, Table 1).

Example 4

A 600 mL reactor fitted with a gas-entrained stirrer (1700 rpm) waspurged 3 times with argon while heated at 50° C. The reactor was thencooled to 30° C. and a solution of MAO (5.90 g, 10 wt % Al) in 63.22 gtoluene, followed by 86.62 g of toluene was transferred via a stainlesssteel cannula to the reactor. The reactor was then pressurized withethylene (35 atmospheres (gauge)) and the temperature adjusted to 45° C.Bis(di-(ortho-fluorophenyl)phosphino)-1-propylamine (17.42 mg, 0.035mmol) in 8.69 g of toluene was added to chromium acetylacetonate (11.78mg, 0.034 mmol) in 8.69 g of toluene in a hypovial. The mixture wassonicated at ambient temperature for 1 minute and then transferred underethylene to the pressurized reactor. Immediately after, additionalethylene was added to increase the reactor pressure to 40 atmospheres(gauge). The reaction was terminated after 10 minutes by stopping theflow of ethylene to the reactor and cooling the contents to 30° C., atwhich point excess ethylene was slowly released from the reactor coolingthe contents to 0° C. The product mixture was transferred to apre-weighed flask containing 1 g of ethanol. A sample of the liquidproduct was analyzed by GC. The solid products were collected, weighedand dried at ambient temperature. The mass of the total product wasobtained by summing the weight of liquid and wet solid fractions (64.3g) (Example 4a, Table 1). This experiment was repeated twice more toensure reproducibility (Examples 4b & 4c, Table 1).

Example 5

A 600 mL reactor fitted with a gas-entrained stirrer (1700 rpm) waspurged 3 times with argon while heated at 50° C. The reactor was thencooled to 30° C. and a solution of MAO (6.15 g, 10 wt % Al) in 62.87 gtoluene, followed by 86.7 g of toluene was transferred via a stainlesssteel cannula to the reactor. The reactor was then pressurized withethylene (15 atmospheres (gauge)) and the temperature adjusted to 45° C.Bis(di-(ortho-fluorophenyl)phosphino)-1-propylamine (17.42 mg, 0.035mmol) in 8.69 g of toluene was added to chromium acetylacetonate (11.79mg, 0.034 mmol) in 8.68 g of toluene in a hypovial. The mixture wassonicated at ambient temperature for 1 minute and then transferred underethylene to the pressurized reactor. Immediately after, additionalethylene was added to increase the reactor pressure to 20 atmospheres(gauge). The reaction was terminated after 20 minutes by stopping theflow of ethylene to the reactor and cooling the contents to 30° C., atwhich point excess ethylene was slowly released from the reactor coolingthe contents to 0° C. The product mixture was transferred to apre-weighed flask containing 1 g of ethanol. A sample of the liquidproduct was analyzed by GC. The solid products were collected, weighedand dried at ambient temperature. The mass of the total product wasobtained by summing the weight of liquid and wet solid fractions (40.3g) (Example 5a, Table 1). See Example 5b, Table 1 for repeat run.

Example 6

A 600 mL reactor fitted with a gas-entrained stirrer (1700 rpm) waspurged 3 times with argon while heated at 50° C. The reactor was thencooled to 30° C. and a solution of MAO (6.05 g, 10 wt % Al) in 62.97 gtoluene, followed by 86.7 g of toluene was transferred via a stainlesssteel cannula to the reactor. The reactor was then pressurized withethylene (5 atmospheres (gauge)) and the temperature adjusted to 45° C.Bis(di-(ortho-fluorophenyl)phosphino)-1-propylamine (17.53 mg, 0.035mmol) in 8.73 g of toluene was added to chromium acetylacetonate (11.62mg, 0.033 mmol) in 8.70 g of toluene in a hypovial. The mixture wassonicated at ambient temperature for 1 minute and then transferred underethylene to the pressurized reactor. Immediately after, additionalethylene was added to increase the reactor pressure to 10 atmospheres(gauge). The reaction was terminated after 20 minutes by stopping theflow of ethylene to the reactor and cooling the contents to 30° C., atwhich point excess ethylene was slowly released from the reactor coolingthe contents to 0° C. The product mixture was transferred to apre-weighed flask containing 1 g of ethanol. A sample of the liquidproduct was analyzed by GC. The solid products were collected, weighedand dried at ambient temperature. The mass of the total product wasobtained by summing the weight of liquid and wet solid fractions (6.5 g)(Example 6, Table 1).

COMPARATIVE EXAMPLE Example 7

A 600 mL reactor fitted with a gas-entrained stirrer (1700 rpm) waspurged 3 times with argon while heated at 50° C. The reactor was thencooled to 30° C. and a solution of MAO (6.09 g, 10 wt % Al) in 62.92 gtoluene, followed by 86.7 g of toluene was transferred via a stainlesssteel cannula to the reactor. The reactor was then pressurized withethylene (35 atmospheres (gauge)) and the temperature adjusted to 45° C.Bis(diphenyl)phosphino)-1-propylamine (15.29 mg, 0.036 mmol) in 10.69 gof toluene was added to chromium acetylacetonate (11.74 mg, 0.034 mmol)in 8.71 g of toluene in a hypovial. The mixture was sonicated at ambienttemperature for 1 minute and then transferred under ethylene to thepressurized reactor. Immediately after, additional ethylene was added toincrease the reactor pressure to 40 atmospheres (gauge). The reactionwas terminated after 16 minutes by stopping the flow of ethylene to thereactor and cooling the contents to 30° C., at which point excessethylene was slowly released from the reactor cooling the contents to 0°C. The product mixture was transferred to a pre-weighed flask containing1 g of ethanol. A sample of the liquid product was analyzed by GC. Thesolid products were collected, weighed and dried at ambient temperature.The mass of the total product was obtained by summing the weight ofliquid and wet solid fractions (63.7 g) (Example 7, Table 1).

TABLE 1 Ethylene Oligomerization Reactions Rx Productivity Total Press.Temp Time (g Product/g Product Wt % Liquid Product Distribution/Wt %Example (atmospheres) (° C.) (min) Cr/hr) Wt (g) PE C4's C6's % 1-C6C8's % 1-C8 C10+ 1 20 45 12 73,638 50.2 1.00 0.97 36.55 99.04 57.6599.65 4.83 2 20 70 21 23,573 28.0 7.14 3.70 33.69 99.49 26.35 98.1036.26 3 40 45 5 166,899 47.2 1.27 0.37 34.53 99.00 60.79 99.63 4.31 4a40 45 10 220,030 64.3 0.78 0.25 23.76 97.02 70.25 99.71 5.75 4b 40 45 11193,672 61.2 0.65 0.22 24.56 97.15 69.17 99.71 6.05 4c 40 45 11 212,87467.5 0.74 0.26 23.76 97.04 70.17 99.72 5.81 5a 20 45 20 68,894 40.3 1.490.46 33.58 97.91 60.84 99.70 5.12 5b 20 45 20 53,946 32.6 4.60 0.5335.93 98.06 58.03 99.67 5.51 6 10 45 20 11,274 6.5 0.00 0.85 49.52 98.7546.41 99.41 3.22 7-c 40 45 16 136,755 63.7 2.35 0.46 21.89 75.51 71.2899.37 5.72

1. The molecule:

wherein R is isopropyl.
 2. A process to prepare the molecule of claim 1,characterized in that said process employs a molecule defined by theformula (ortho —F—C₆H₄)₂PX wherein X is a halide selected from the groupconsisting of chlorine and bromine.
 3. The process of claim 2comprising: 1) preparing an intermediate by reacting said moleculedefined by the formula (ortho —F—C₆H₄)₂PX with a reactant selected fromthe group consisting of a) isopropyl amine and b) an isopropyl amidedefined by the formula (M¹)(iPr)NH wherein iPr is isopropyl and M¹ isselected from the group consisting of lithium, sodium, magnesium andzinc; 2) deprotonating said intermediate; and 3) reacting thedeprotonated intermediate from step 2 with said molecule defined by theformula (ortho-F—C₆H₄)₂PX.
 4. A process for the oligomerization ofethylene to a mixture comprising hexene-1 and octene-1, said processcomprising contacting ethylene under oligomerization reaction conditionswith a catalyst system to produce an oligomerization product comprisinghexene-1 and octene-1, said catalyst system comprising: i) a source ofchromium; ii) a ligand defined by the formula

wherein each of X₁ to X₄ is independently selected from the groupconsisting of F, Br, or Cl; and each of R; ort¹ to ort⁴ and R₁ to R₁₂ isindependently selected from the group consisting of H andnon-interfering substituents; and iii) an activator.
 5. The process ofclaim 4 wherein said activator is methalumoxane.
 6. The process of claim3 wherein said mixture comprising hexene-1 and octene-1 is furthercontacted with a polymerization catalyst.
 7. The process of claim 3wherein said mixture comprising hexene-1 and octene-1 is separated bydistillation to produce a hexene-1 product.
 8. The process of claim 7wherein said distillation is undertaken in the distillation system of aconventional alpha olefin plant and wherein said mixture comprisinghexene-1 and octene-1 is added to a crude alpha olefin product from saidconventional alpha olefin plant prior to being added to saiddistillation system.
 9. The process according to claim 3 wherein saidmixture comprising hexene-1 and octene-1 contains less than 10 weight %internal olefins.
 10. The process according to claim 3 wherein saidmixture comprising hexene-1 and octene-1 contains at least 20 weight %octene-1.
 11. The process according to claim 3 wherein said mixturecomprising hexene-1 and octene-1 contains less than 10 weight % internalolefins and at least 20 weight % octene-1.
 12. The process according toclaim 4 when undertaken at a gauge pressure of from 10 to 50atmospheres.
 13. The process according to claim 3 when undertaken at atemperature of from 20 to 70° C.
 14. The process according to claim 4wherein each of said X₁ to X₄ ⁻; ort¹ to ort⁴ and R₁ to R₉ is hydrogenand R is isopropyl.